Method for continuously producing fluorobenzene

Abstract

The invention discloses a method for continuously producing fluorobenzene, which comprises the following steps: S10) mixing anhydrous hydrogen fluoride and aniline in a tubular reactor to obtain an aniline hydrofluoride mixture; s20) introducing the aniline hydrofluoride mixture into a venturi tube reactor in an inert gas atmosphere, sucking powdered and dried sodium nitrite into the venturi tube reactor in a negative pressure environment formed by the venturi tube reactor, and carrying out a synthetic reaction to obtain a diazonium solution; s30) transferring the diazonium solution into a tubular reactor for pyrolytic reaction to obtain a crude fluorobenzene solution; s40) refining the crude fluorobenzene raw material to obtain fluorobenzene; according to the method disclosed by the invention, the crossing from an intermittent artificial kettle reaction to a continuous reaction is realized, the reaction is sufficient and complete, no 70% hydrofluoric acid mother liquor, no 70% sulfuric acid waste liquor, no high-concentration wastewater and no yellow mud solid waste are produced, a high-quality fluorobenzene product can be continuously prepared in a large batch, and the method has good economic and environmental benefits and a wide market application prospect.

Description

Technical Field

[0001] The invention belongs to the field of fluorobenzene preparation, and particularly relates to a method for continuously producing fluorobenzene. Background Art

[0002] my country's fluorobenzene industry has developed rapidly and has gradually become the main supplier of the global fluorobenzene industry, with strong market competitiveness in the global fluorobenzene industry. In recent years, the fluorobenzene industry has generally adopted anhydrous hydrogen fluoride production technology, which has completely changed the backward situation of water production in the past. The anhydrous hydrogen fluoride production process mainly adopts kettle reaction, that is, the raw material anhydrous hydrogen fluoride is added to the reactor, and it needs to be stirred for more than 6 hours for the dropwise addition of aniline. After the dropwise addition of aniline, it takes more than 12 hours to add nitrite, and finally more than 6 hours for decomposition to obtain crude fluorobenzene. The total reaction time of each kettle exceeds 35 hours, and auxiliary operations such as pure manual loading and unloading are required. The operating cost is high, and the product quality is not easy to stabilize. Only small batches of fluorobenzene can be produced; in addition, the entire production process of the fluorobenzene industry will add excessive hydrogen fluoride to ensure the yield, thus producing a large amount of waste acid with complex components, which is difficult to post-process.

[0003] Therefore, the applicant hopes to seek technical solutions to solve the above technical problems. Summary of the invention

[0004] In view of this, the purpose of the present invention is to provide a method for continuously producing fluorobenzene, which realizes the transition from intermittent artificial autoclave reaction to continuous reaction, the reaction is fully and completely, there is no output of 70% hydrofluoric acid mother liquor, 70% sulfuric acid waste liquid, high-concentration wastewater, and yellow mud solid waste, and high-quality fluorobenzene products can be prepared continuously and in large quantities, which has good economic and environmental benefits and broad market application prospects.

[0005] The technical solution adopted by the present invention is as follows: A method for continuously producing fluorobenzene comprises the following steps: S10), mixing anhydrous hydrogen fluoride and aniline in a tubular reactor to obtain an aniline hydrofluoride mixture; S20), introducing the aniline hydrofluoride mixture obtained in the above step S10) into a venturi tube reactor under an inert gas atmosphere, and at the same time sucking the powdered and dried sodium nitrite into the venturi tube reactor under the negative pressure environment formed by the venturi tube reactor, and synthesizing the reaction to obtain a diazo liquid; S30), transferring the diazo solution obtained in the above step S20) to a tubular reactor for pyrolysis reaction to obtain a crude fluorobenzene solution; S40), the crude fluorobenzene raw material obtained in the above step S30) is refined to obtain fluorobenzene.

[0006] Preferably, the tubular reactor in step S10) is a multi-module combined channel structure, and is made of silicon carbide.

[0007] Preferably, in the step S10), the anhydrous hydrogen fluoride and the aniline are fed into the tubular reactor at a molar ratio of 1:1; wherein the total feed rate is preferably 180-220 kg / h, and the temperature range in the tubular reactor is 4-8°C, more preferably 5-6°C.

[0008] Preferably, in the step S20), the venturi tube reactor is made of PFA; and / or the differential ratio of the sodium nitrite when the particle size is 40 μm is not less than 40%, and the cumulative ratio is not less than 85%.

[0009] Preferably, in the step S20), aniline hydrofluoride and sodium nitrite are fed into the venturi reactor at a molar ratio of 1:1.

[0010] Preferably, in the step S20), the inert gas is high-purity nitrogen, and the temperature in the venturi reactor is -3 to 3°C.

[0011] Preferably, the tubular reactor in step S30) adopts a multi-stage series tubular reactor unit combination structure, the temperature in each tubular reactor unit is different and tends to increase; and each tubular reactor unit is provided with a nitrogen discharge outlet.

[0012] Preferably, the tubular reactor of step S30) comprises a first-stage tubular reactor unit, a second-stage tubular reactor unit and a third-stage tubular reactor unit connected in series; wherein the temperature inside the first-stage tubular reactor unit is 6-10°C, the temperature inside the second-stage tubular reactor unit is 18-22°C, and the temperature inside the third-stage tubular reactor unit is 36-45°C.

[0013] Preferably, the tubular reactor unit is a multi-module combined channel structure, and is made of silicon carbide.

[0014] Preferably, the step S40) comprises: using a distillation tower to perform distillation treatment on the crude fluorobenzene raw material to remove moisture from the crude fluorobenzene raw material; the purity of the obtained fluorobenzene is ≥99%.

[0015] It should be particularly noted that the "PFA" involved in the full text of this application is the abbreviation of Polyfluoroalkoxy in English, and its Chinese meaning is: tetrafluoroethylene-perfluoroalkoxy vinyl ether copolymer (also known as: perfluoroalkyl compound, soluble polytetrafluoroethylene); the "tubular reactor or tubular reactor unit with a multi-module combined channel structure" and "Venturi tube reactor" involved in the full text of this application are all well-known reaction devices for those skilled in the art, and the scheme of the reaction device structure itself is not regarded as a separate innovative content of this application. Therefore, these reaction device structure schemes will not be specifically explained.

[0016] The present application realizes a transition from intermittent artificial kettle reaction to continuous reaction. The reaction is fully and completely, and there is no output of 70% hydrofluoric acid mother liquor, 70% sulfuric acid waste liquid, high-concentration wastewater, and yellow mud solid waste. High-quality fluorobenzene products can be prepared continuously and in large quantities, which has good economic and environmental benefits and broad market application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a flowchart of the steps of the method for continuous production of fluorobenzene under a specific embodiment of the present invention; Figure 2 It is a schematic diagram of the connection status of equipment for continuous production of fluorobenzene according to a specific embodiment of the present invention. DETAILED DESCRIPTION

[0018] See also Figure 1 Combined with Figure 2 As shown, this embodiment provides a method for continuously producing fluorobenzene, comprising the following steps: S10), mixing anhydrous hydrogen fluoride and aniline in a tubular reactor to obtain an aniline hydrofluoride mixture. In this step, the tubular reactor can achieve a molecular-level mixing effect, so that the anhydrous hydrogen fluoride and aniline are dispersed at the micron scale, dispersed into micron-scale thin streams, and collided and mixed according to a preset ratio; preferably, the tubular reactor in this step is a multi-module combined channel structure, and is made of silicon carbide; preferably, in this step, anhydrous hydrogen fluoride and aniline are fed to the tubular reactor at a molar ratio of 1:1, and the reaction is fully carried out according to the reaction equation of C6H7N+HF→C6H8NF; preferably, in this step, the total feed amount is preferably 180-220kg / h (too low will affect the product yield, too high will affect the product yield and product purity), and the temperature range in the tubular reactor is 4-8°C, more preferably 5-6°C; S20), introducing the aniline hydrofluoride mixture obtained in the above step S10) into a venturi reactor under an inert gas atmosphere, and at the same time, sucking the powdered and dried sodium nitrite into the venturi reactor under the negative pressure environment formed by the venturi reactor, and synthesizing the diazo liquid, which is output to the tubular reactor in the next step S30) through the outlet of the venturi reactor; it should be noted that, in combination with the Bernoulli principle and the fluid continuity equation, it can be known that for the liquid aniline hydrofluoride mixture, the flow rate will increase and the pressure will decrease at the narrow part, so the narrow part of the venturi reactor plays a role of vacuuming, and the inert gas is introduced. Aniline hydrofluoride mixture is added to produce a vacuum effect (i.e., a negative pressure environment is formed); preferably, in this step, aniline hydrofluoride and sodium nitrite are fed into the venturi reactor at a molar ratio of 1:1, and the feed is strictly in accordance with the reaction equation of C6H8NF+NaNO2→C6H5N2F; the venturi reactor is made of PFA; and / or preferably, in this step, the differential ratio of sodium nitrite when the particle size is 40 μm is not less than 40%, and the cumulative ratio is not less than 85%; preferably, in this step, high-purity nitrogen is used as the inert gas, and the temperature in the venturi reactor is -3 to 3°C, more preferably -1 to 1°C; S30), transferring the diazo liquid obtained in the above step S20) to a tubular reactor for pyrolysis reaction to obtain a crude fluorobenzene solution, wherein the tubular reactor can achieve a molecular-level mixing effect, so that the diazo liquid is dispersed at the micron scale and dispersed into micron-scale thin streams; preferably, the tubular reactor in this step adopts a multi-stage series tubular reactor unit combination structure, and the temperature in each tubular reactor unit is different and tends to increase; and each tubular reactor unit is provided with a nitrogen discharge outlet; further preferably, the tubular reactor in this step S30) includes a first-stage tubular reactor unit, a second-stage tubular reactor unit and a third-stage tubular reactor unit connected in series; wherein the temperature in the first-stage tubular reactor unit is 6-10°C, the temperature in the second-stage tubular reactor unit is 18-22°C, and the temperature in the third-stage tubular reactor unit is 36-45°C; preferably, the tubular reactor unit in this step is a multi-module combined channel structure, and is made of silicon carbide; S40), refining the crude fluorobenzene raw material obtained in the above step S30) to obtain fluorobenzene; preferably, this step S40) includes: using a distillation tower (preferably made of PFA material) to distill the crude fluorobenzene raw material, and distilling at the boiling point of fluorobenzene to remove moisture from the crude fluorobenzene raw material; the purity of the obtained fluorobenzene is ≥99%, more preferably ≥99.9%, further preferably ≥99.95%, and further preferably ≥99.99%.

[0019] In order to enable those skilled in the art to better understand the technical solutions in the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work should fall within the scope of protection of the present invention.

[0020] On the basis of the above implementation contents, in order to verify the technical effects achieved by the present application, the present application further proposes the following embodiments and comparative examples: Example

[0021] A tubular reactor having a multi-module combined continuous channel structure and made of silicon carbide is selected as the tubular reactor in step S10) of this embodiment; A venturi tube reactor made of PFA material is selected as the venturi tube reactor in step S20) of this embodiment; A tubular reactor having a multi-module combined continuous channel structure and made of silicon carbide is selected as the first-stage tubular reactor unit, the second-stage tubular reactor unit and the third-stage tubular reactor unit in step S30) of this embodiment; A plate-type distillation tower made of PFA material is selected as the distillation tower in step S40) of this embodiment; This embodiment prepares fluorobenzene according to the following process: S10). Continuously feeding anhydrous hydrogen fluoride and aniline into a tubular reactor respectively, and reacting to obtain an aniline hydrofluoride solution; wherein the feed molar ratio of anhydrous hydrogen fluoride to aniline is 1:1, and the total feed amount of anhydrous hydrogen fluoride and aniline is 200 kg / h, the temperature in the tubular reactor is set to 5° C., and after the reaction is completed, an aniline hydrofluoride mixture is obtained; S20). The aniline hydrofluoride mixture obtained in the above step S10) is introduced into a venturi reactor under a high-purity nitrogen atmosphere (purity greater than 99.999%), and at the same time, powdered and dried sodium nitrite (the differential ratio of sodium nitrite when the particle size is 40 μm is 50%, and the cumulative ratio is 90%) is sucked into the venturi reactor at a temperature of 0°C under the negative pressure environment formed by the venturi reactor, and a synthetic reaction is performed to obtain a diazo liquid; S30). The diazo liquid obtained in the above step S20) is transferred to a tubular reactor for pyrolysis reaction to obtain a crude fluorobenzene solution; wherein, the tubular reactor in this step includes a first-stage tubular reactor unit, a second-stage tubular reactor unit and a third-stage tubular reactor unit connected in series; wherein, the temperature in the first-stage tubular reactor unit is 8°C, the temperature in the second-stage tubular reactor unit is 20°C, and the temperature in the third-stage tubular reactor unit is 40°C, so that the diazo liquid is gradually decomposed in the three temperature sections to obtain a crude fluorobenzene solution; S40). The crude fluorobenzene raw material obtained in the above step S30) is transported to a distillation tower, and the distillation tower performs distillation treatment on the crude fluorobenzene raw material at the boiling point temperature of fluorobenzene (specifically set to 85° C.) to obtain high-purity liquid fluorobenzene.

[0022] According to the detection of Agilent 7890A gas chromatograph, the purity of high-purity liquid fluorobenzene is 99.992%, the water content is 35ppm, and the yield is greater than 99.99% (close to 100%); subsequently, the continuously produced high-purity liquid fluorobenzene can be cooled in the product cooler and then enter the fluorobenzene liquid collecting tank; This embodiment 1 realizes the continuous batch production of high-purity liquid fluorobenzene, and there is no output of 70% hydrofluoric acid mother liquor, 70% sulfuric acid waste liquid, high-concentration wastewater, and yellow mud solid waste.

[0023] Example 2: The rest of the technical scheme of Example 2 is the same as that of Example 1, with the only difference being that, in Example 2, the total feed rate in step S10) is set to 180 kg / h, and the temperature in the tubular reactor is 4°C; as detected by gas chromatograph, the purity of the high-purity liquid fluorobenzene obtained in Example 2 is 99.994%, and the yield is greater than 99.99%.

[0024] Example 3: The rest of the technical scheme of Example 3 is the same as that of Example 1, with the only difference being that, in Example 3, the total feed rate in step S10) is set to 220 kg / h, and the temperature in the tubular reactor is 6°C; as detected by gas chromatograph, the purity of the high-purity liquid fluorobenzene obtained in Example 3 is 99.991%, and the yield is greater than 99.99%.

[0025] Example 4: The remaining technical solutions of Example 4 are the same as those of Example 1, with the only difference being that, in Example 4, the temperature in the Venturi tube reactor in step S20) is set to -3°C; as detected by gas chromatograph, the purity of the high-purity liquid fluorobenzene obtained in Example 4 is 99.991%, and the yield is greater than 99.99%.

[0026] Example 5: The rest of the technical scheme of Example 5 is the same as that of Example 1, with the only difference being that, in Example 5, the temperature in the Venturi tube reactor in step S20) is set to 3°C; as detected by gas chromatograph, the purity of the high-purity liquid fluorobenzene obtained in Example 5 is 99.99%, and the yield is greater than 99.99%.

[0027] Embodiment 6: The remaining technical solutions of Embodiment 6 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 6, the temperature in the first-stage tubular reactor unit is 6°C, the temperature in the second-stage tubular reactor unit is 18°C, and the temperature in the third-stage tubular reactor unit is 36°C; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in Example 6 is 99.991%, and the yield is greater than 99.99%.

[0028] Embodiment 7: The remaining technical solutions of Embodiment 7 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 7, the temperature in the first-stage tubular reactor unit is 10° C., the temperature in the second-stage tubular reactor unit is 22° C., and the temperature in the third-stage tubular reactor unit is 45° C.; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 7 is 99.99%, and the yield is greater than 99.99%.

[0029] Example 8: The rest of the technical scheme of Example 8 is the same as that of Example 1, with the only difference being that, in Example 8, the total feed rate in step S10) is set to 260 kg / h, and the temperature in the tubular reactor is 1°C; as detected by gas chromatograph, the purity of the high-purity liquid fluorobenzene obtained in Example 8 is 99.96%, and the yield is 99.2%.

[0030] Example 9: The rest of the technical scheme of Example 9 is the same as that of Example 1, with the only difference being that, in Example 9, the temperature in the Venturi tube reactor in step S20) is set to -5°C; as detected by gas chromatograph, the purity of the high-purity liquid fluorobenzene obtained in Example 9 is 99.94%, and the yield is about 99%.

[0031] Embodiment 10: The remaining technical solutions of Embodiment 10 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 10, the temperature in the first-stage tubular reactor unit is 0°C, the temperature in the second-stage tubular reactor unit is 8°C, and the temperature in the third-stage tubular reactor unit is 20°C; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 10 is 99.96%, and the yield is less than 95%.

[0032] Embodiment 11: The remaining technical solutions of Embodiment 11 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 11, the temperature in the first-stage tubular reactor unit is 40° C., the temperature in the second-stage tubular reactor unit is 20° C., and the temperature in the third-stage tubular reactor unit is 8° C.; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 11 is about 99.2%, and the yield is less than 90%.

[0033] Embodiment 12: The remaining technical solutions of Embodiment 12 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 12, the temperature in the first-stage tubular reactor unit is 20° C., the temperature in the second-stage tubular reactor unit is 20° C., and the temperature in the third-stage tubular reactor unit is 40° C.; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 12 is 99.8%, and the yield is 99.6%.

[0034] Embodiment 13: The remaining technical solutions of Embodiment 13 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 13, the temperature in the first-stage tubular reactor unit is 40° C., the temperature in the second-stage tubular reactor unit is 40° C., and the temperature in the third-stage tubular reactor unit is 40° C.; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 13 is 99.92%, and the yield is 99.1%.

[0035] Example 14: The remaining technical solutions of Example 14 are the same as those of Example 1, except that, in step S30 of Example 14, the tubular reactor comprises a first-stage tubular reactor unit and a second-stage tubular reactor unit connected in series, wherein the temperature in the first-stage tubular reactor unit is 20°C, and the temperature in the second-stage tubular reactor unit is 40°C; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 14 is 99.94%, and the yield is 99.5%.

[0036] Example 15: The remaining technical solutions of Example 15 are the same as those of Example 1, except that, in step S30 of Example 15, the tubular reactor comprises a first-stage tubular reactor unit and a second-stage tubular reactor unit connected in series, wherein the temperature in the first-stage tubular reactor unit is 8°C, and the temperature in the second-stage tubular reactor unit is 40°C; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 15 is 99.91%, and the yield is 99.3%.

[0037] Embodiment 16: The remaining technical solutions of Embodiment 16 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 16, the tubular reactor includes a first-stage tubular reactor unit, wherein the temperature in the first-stage tubular reactor unit is 20°C; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 16 is about 99%, and the yield is 99%.

[0038] Embodiment 17: The remaining technical solutions of Embodiment 17 are the same as those of Embodiment 1, except that, in step S30 of Embodiment 17, the tubular reactor includes a first-stage tubular reactor unit, wherein the temperature in the first-stage tubular reactor unit is 40°C; According to the gas chromatograph detection, the purity of the high-purity liquid fluorobenzene obtained in this Example 17 is 99.5%, and the yield is 99.5%.

[0039] Comparative Example 1: The rest of the technical scheme of this comparative example 1 is the same as that of Example 1, with the only difference being that, in this comparative example 1, the tubular reactor in step S10) and step S30) and the venturi tube reactor in step S20) are all replaced by reactors, that is, step S10), step S20) and step S30) are all reacted in the same reactor to obtain crude fluorobenzene; the preparation process is intermittent and cannot be continuous, the total reaction time of each reactor exceeds 35 hours, and a large amount of waste acid with complex components will be produced.

[0040] Comparative Example 2: The remaining technical solutions of this comparative example 2 are the same as those of Example 1, except that, in this comparative example 2, the venturi tube reactor in step S20) is replaced by the same tubular reactor as in step 10); According to the gas chromatograph detection, the purity of the liquid fluorobenzene obtained in this comparative example 2 is 92.5%, and the yield is about 95.4%.

[0041] It will be apparent to those skilled in the art that the invention is not limited to the details of the exemplary embodiments described above and that the invention can be implemented in other specific forms without departing from the spirit or essential features of the invention. Therefore, the embodiments should be considered exemplary and non-limiting in all respects, and the scope of the invention is defined by the appended claims rather than the foregoing description, and it is intended that all variations falling within the meaning and scope of the equivalent elements of the claims be included in the invention. Any reference numeral in a claim should not be considered as limiting the claim to which it relates.

[0042] In addition, it should be understood that although the present specification is described according to implementation modes, not every implementation mode contains only one independent technical solution. This description of the specification is only for the sake of clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment may also be appropriately combined to form other implementation modes that can be understood by those skilled in the art.

Claims

1. A method for continuously producing fluorobenzene, characterized in that: The steps include: S10), mixing anhydrous hydrogen fluoride and aniline in a tubular reactor to obtain an aniline hydrofluoride mixture; S20), introducing the aniline hydrofluoride mixture obtained in the above step S10) into a venturi tube reactor under an inert gas atmosphere, and at the same time sucking the powdered and dried sodium nitrite into the venturi tube reactor under the negative pressure environment formed by the venturi tube reactor, and synthesizing the reaction to obtain a diazo liquid; S30), transferring the diazo solution obtained in the above step S20) to a tubular reactor for pyrolysis reaction to obtain a crude fluorobenzene solution; S40), the crude fluorobenzene raw material obtained in the above step S30) is refined to obtain fluorobenzene.

2. The method for continuous production of fluorobenzene according to claim 1, characterized in that: The tubular reactor in step S10) is a multi-module combined channel structure, and is made of silicon carbide.

3. The method for continuous production of fluorobenzene according to claim 1, characterized in that: In the step S10), the anhydrous hydrogen fluoride and the aniline are fed into the tubular reactor at a molar ratio of 1:1; wherein the total feed rate is preferably 180-220 kg / h, and the temperature range in the tubular reactor is 4-8°C, more preferably 5-6°C.

4. The method for continuous production of fluorobenzene according to claim 1, characterized in that: In the step S20), the venturi tube reactor is made of PFA; and / or the differential ratio of the sodium nitrite when the particle size is 40 μm is not less than 40%, and the cumulative ratio is not less than 85%.

5. The method for continuous production of fluorobenzene according to claim 1, characterized in that: In the step S20), aniline hydrofluoride and sodium nitrite are fed into the venturi reactor at a molar ratio of 1:

1.

6. The method for continuous production of fluorobenzene according to claim 1, characterized in that: In the step S20), the inert gas is high-purity nitrogen, and the temperature in the venturi reactor is -3 to 3°C.

7. The method for continuous production of fluorobenzene according to claim 1, characterized in that: The tubular reactor in step S30) adopts a multi-stage series-connected tubular reactor unit combination structure, the temperature in each tubular reactor unit is different and tends to increase; and each tubular reactor unit is provided with a nitrogen discharge outlet.

8. The method for continuous production of fluorobenzene according to claim 7, characterized in that: The tubular reactor of step S30) comprises a first-stage tubular reactor unit, a second-stage tubular reactor unit and a third-stage tubular reactor unit connected in series; wherein the temperature inside the first-stage tubular reactor unit is 6-10°C, the temperature inside the second-stage tubular reactor unit is 18-22°C, and the temperature inside the third-stage tubular reactor unit is 36-45°C.

9. The method for continuous production of fluorobenzene according to claim 6, characterized in that: The tubular reactor unit is a multi-module combined channel structure and is made of silicon carbide.

10. The method for continuous production of fluorobenzene according to claim 1, characterized in that: The step S40) includes: using a distillation tower to perform distillation treatment on the crude fluorobenzene raw material to remove moisture from the crude fluorobenzene raw material; the purity of the obtained fluorobenzene is ≥99%.

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